CN104312625A - Energy-saving type wax oil hydrogenation equipment in petrochemical industry - Google Patents
Energy-saving type wax oil hydrogenation equipment in petrochemical industry Download PDFInfo
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- CN104312625A CN104312625A CN201410520678.2A CN201410520678A CN104312625A CN 104312625 A CN104312625 A CN 104312625A CN 201410520678 A CN201410520678 A CN 201410520678A CN 104312625 A CN104312625 A CN 104312625A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses energy-saving type wax oil hydrogenation equipment in petrochemical industry. The energy-saving type wax oil hydrogenation equipment comprises a hydrogenation reactor, an oil separating unit, a hydrogen-sulfide-removal stripping tower and a top reflux tank of the hydrogen-sulfide-removal stripping tower, wherein a bottom outlet end of a cold low-pressure separator in the oil separating unit is connected with diesel oil hydrogenation equipment by virtue of a pipeline; the hydrogen-sulfide-removal stripping tower is connected with the top reflux tank of the hydrogen-sulfide-removal stripping tower; a top outlet end of the hydrogen-sulfide-removal stripping tower is communicated with the top reflux tank of the hydrogen-sulfide-removal stripping tower by virtue of a pipeline; a bottom outlet end of the hydrogen-sulfide-removal stripping tower is communicated with a wax oil pipeline; and the outlet of the top reflux tank of the hydrogen-sulfide-removal stripping tower is divided into three branches, wherein one branch is communicated with a dry gas exhausting pipeline, one branch is communicated with the upper part of the hydrogen-sulfide-removal stripping tower and another branch is connected with the hydrogen-sulfide-removal stripping tower of the adjacent diesel oil hydrogenation equipment by virtue of a pipeline or the hydrogen-sulfide-removal stripping tower of petroleum hydrogenation equipment. The wax oil hydrogenation equipment achieves the purpose of lowering the energy consumption of the equipment while satisfying the oil separating effect.
Description
Technical field
The present invention relates to the refining equipment in petrochemical complex, specifically refer to energy-saving Wax Oil Hydrogenation Unit in petrochemical complex.
Background technology
Wax Oil Hydrogenation Unit is the important device in petrochemical complex, Wax Oil Hydrogenation Unit common in prior art as shown in Figure 1, comprise reaction heating furnace 1, hydrogenator 2, oil product separating unit, depriving hydrogen sulphide stripping tower 7, hydrogen rich gas thionizer 8, depriving hydrogen sulphide stripping return tank of top of the tower 13, fractionation process furnace 14, separation column 15, fractionation return tank of top of the tower 16 and diesel oil stripping tower 17, enter Wax Oil Hydrogenation Unit with the mixing raw material oil of catalytic diesel oil by stock oil pipeline containing decompressed wax oil carry out hydrogenation reaction and be separated, finally obtain refining wax oil by separation column 15, diesel oil is obtained by diesel oil stripping tower 17, petroleum naphtha is obtained by fractionation return tank of top of the tower 16, hydrogen rich gas thionizer 8 is for absorbing hydrogen sulphide, methane and ethane mixed gas, and carry out desulphurization reaction by the poor amine liquid of splendid attire in tower and hydrogen sulfide, obtain methane and the ethane mixed gas of purification.
Mixing raw material oil enters the top inlet end of hydrogenator 2 after reaction heating furnace 1, in hydrogenator 2, carry out hydrogenation reaction, generates the mixing oil product that comprises petroleum naphtha, refining wax oil and diesel oil and comprises the mixed gas of hydrogen sulfide and methane, ethane.Oil product separating unit is by high pressure hot separator 3, thermal low-pressure separators 4, cold high pressure separator 5 and cold low separator 6 form, the exit end of hydrogenator 2 is connected with the entrance end of high pressure hot separator 3, the exit end of high pressure hot separator 3 is divided into two-way, top exit end is connected with the entrance end of cold high pressure separator 5, hot high score gas air cooler 11 is also provided with between high pressure hot separator 3 top exit end and the entrance end of cold high pressure separator 5, the outlet at bottom end of high pressure hot separator 3 is connected with the entrance end of thermal low-pressure separators 4, the product that hydrogenator 2 hydrogenation reaction obtains is separated in high pressure hot separator 3, the refining wax oil that proportion is heavier and a small amount of diesel oil enter in thermal low-pressure separators 4, the petroleum naphtha that proportion is lighter, comprise hydrogen sulfide and methane, mixed gas and a large amount of diesel oil of ethane enter cold high pressure separator 5, the exit end of cold high pressure separator 5 is divided into two-way, be respectively outlet at bottom end and top exit end, be connected by return line between top exit end with stock oil pipeline, return line is disposed with desulphurization of recycle hydrogen tower 9 and circulating hydrogen compressor 10 along from cold high pressure separator 5 top exit end on the direction of stock oil pipeline, the hydrogen sulfide that desulphurization of recycle hydrogen tower 9 is brought out by poor amine liquid and cold high pressure separator 5 top exit of splendid attire in tower carries out desulphurization reaction, the pipeline section of return line after circulating hydrogen compressor 10 be the pipeline that is connected with the entrance end of hydrogenator 2 of collateral branch one tunnel also, the hydrogen that desulphurization reaction is produced adds in hydrogenator 2 again, the outlet at bottom end of cold high pressure separator 5 is connected with the entrance end of cold low separator 6, the exit end of thermal low-pressure separators 4 is divided into two-way, top exit end is connected with the entrance end of cold low separator 6, heat low point of gas air cooler 12 is also provided with between the top exit end of thermal low-pressure separators 4 and the entrance end of cold low separator 6, the outlet at bottom end of thermal low-pressure separators 4 is connected with depriving hydrogen sulphide stripping tower 7 by pipeline, the oil product entering depriving hydrogen sulphide stripping tower 7 from thermal low-pressure separators 4 outlet at bottom end is essentially refining wax oil, a small amount of diesel oil enters cold low separator 6 by top exit end.
Cold low separator 6 is by the petroleum naphtha of acquisition, diesel oil and comprise hydrogen sulfide and be separated with the mixed gas of methane, ethane, the exit end of cold low separator 6 is divided into two-way, top exit end is connected with dry gas discharge pipe, by dry gas discharge pipe, the methane in mixed gas, ethane gas are discharged, cold low separator 6 outlet at bottom end is connected with depriving hydrogen sulphide stripping tower 7 by pipeline, for the mixing oil product of diesel oil higher for purity and petroleum naphtha is flowed to depriving hydrogen sulphide stripping tower 7.Depriving hydrogen sulphide stripping tower 7 is connected with depriving hydrogen sulphide stripping return tank of top of the tower 13, the top exit end of depriving hydrogen sulphide stripping tower 7 is connected by pipeline with depriving hydrogen sulphide stripping return tank of top of the tower 13, the outlet at bottom end of depriving hydrogen sulphide stripping tower 7 is connected with fractionation process furnace 14, fractionation process furnace 14 is connected with separation column 15, and refining wax oil, the diesel oil of mixing enter in separation column 15 with petroleum naphtha and is separated mixing oil product after fractionation process furnace 14.
The outlet of separation column 15 is divided into three tunnels, one tunnel is bottom end outlet end, be connected with wax oil pipeline, for exporting the refining wax oil after separation, a road be top exit end, be connected with fractionation return tank of top of the tower 16, for exporting the petroleum naphtha after separation, another road is centre exit end, is connected with diesel oil stripping tower 17, for exporting the diesel oil after separation.
In above-mentioned Wax Oil Hydrogenation Unit, the mixing raw material oil of decompressed wax oil and catalytic diesel oil enters Wax Oil Hydrogenation Unit, through adding supercharging, heat exchange, after filtration after the boosting of hydrogenation fresh feed pump with mix hydrogen and mix, successively through reaction effluent/parallel feeding interchanger, reaction feed process furnace be heated to reaction temperature required after enter hydrogenator and carry out hydrogenation reaction, by the sulphur in raw material, nitrogen, the converting compounds such as oxygen are hydrogen sulfide, ammonia, water, to alkene, aromatic hydrocarbons carries out hydrotreated lube base oil, remove the metal impurities in raw material, carry out partial cracking reaction simultaneously, generate petroleum naphtha and diesel oil.By reactor reaction effluent out after heat exchange, enter that high pressure hot separator carries out gas, liquid is separated.Bottom high pressure hot separator, hot high score oil out enters thermal low-pressure separators under Liquid level after hydrogenation fresh feed pump hydraulic turbine recovered energy; Heat low point of oil enters depriving hydrogen sulphide stripping tower, with 1.0MPa superheated vapour stripping at the bottom of tower after mixing with cold low point of oil.Oil phase through depriving hydrogen sulphide stripping tower top reflux pump boosting after all as trim the top of column.Depriving hydrogen sulphide stripping tower bottom oil enters separation column charging process furnace after the boosting of depriving hydrogen sulphide stripping tower bottom pump after wax oil/separation column feed exchanger heat exchange, enters product separation column after being heated to 385 DEG C.Tower top oil gas warp, a part is as the backflow of separation column, and another part goes out device as raw naphtha product.The oily(waste)water dividing water bag to discharge recycles through oily(waste)water pump.Diesel oil distillate enters diesel oil stripping tower from separation column the 18th layer of tower tray.Diesel oil stripping top gaseous phase returns on separation column the 15th layer of tower tray, after liquid phase at the bottom of tower reclaims heat further as diesel product diesel oil, is cooled to 60 DEG C and goes out device.Diesel oil stripping tower adopts (thermal source the is wax oil product) stripping that heavily boils, and product Fractionator Bottom oil, through the boosting of wax oil pump, is normally refined hot wax oil 165 DEG C of conducts and directly delivered to catalytic cracking unit; Or after wax oil air cooler is cooled to 90 DEG C, deliver to tank field again.
Refine because wax oil hydrogenation technique belongs to oil hydrogenation, its main purpose is the impurity such as the sulphur removed in wax oil, oxygen, for downstream catalytic cracking unit provides the raw material of low-sulfur.The diesel oil that meeting by-product is a small amount of in hydrogenation process and petroleum naphtha component, these diesel oil and petroleum naphtha component are blended in refining wax oil, as taken in downstream catalytic cracking unit, the dry gas yied adding catalytic cracking unit being caused Value Loss, therefore having to pass through separation column and separating from refining wax oil.Due to the diesel oil of this part by-product and the yield of petroleum naphtha itself very low, but to be separated by separation column, cause plant energy consumption high.
Summary of the invention
The object of this invention is to provide energy-saving Wax Oil Hydrogenation Unit in petrochemical complex, this Wax Oil Hydrogenation Unit, by the improvement to circuit, while meeting oil product separating effect, reaches the object reducing plant energy consumption.
Above-mentioned purpose of the present invention realizes by the following technical solutions: energy-saving Wax Oil Hydrogenation Unit in petrochemical complex, comprise hydrogenator, oil product separating unit, depriving hydrogen sulphide stripping tower and depriving hydrogen sulphide stripping return tank of top of the tower, described oil product separating unit is by high pressure hot separator, thermal low-pressure separators, cold high pressure separator and cold low separator composition, the exit end of described hydrogenator is connected with the entrance end of high pressure hot separator, the exit end of high pressure hot separator is divided into two-way, top exit end is connected with the entrance end of cold high pressure separator, outlet at bottom end is connected with the entrance end of thermal low-pressure separators, described cold high pressure separator has outlet at bottom end, outlet at bottom end is connected with the entrance end of cold low separator, the exit end of described thermal low-pressure separators is divided into two-way, top exit end is connected with the entrance end of cold low separator, outlet at bottom end is connected with depriving hydrogen sulphide stripping tower by pipeline, the exit end of described cold low separator is divided into two-way, top exit end is connected with dry gas discharge pipe, it is characterized in that: described cold low separator bottom exit end is connected with diesel hydrotreating unit by pipeline, described depriving hydrogen sulphide stripping tower is connected with depriving hydrogen sulphide stripping return tank of top of the tower, the top exit end of depriving hydrogen sulphide stripping tower is connected by pipeline with depriving hydrogen sulphide stripping return tank of top of the tower, the outlet at bottom end of depriving hydrogen sulphide stripping tower is connected with wax oil pipeline, the outlet of described depriving hydrogen sulphide stripping return tank of top of the tower is divided into three tunnels, one tunnel is connected with described dry gas discharge pipe, one tunnel is connected with the top of depriving hydrogen sulphide stripping tower, a partitioning cycle loop is formed with depriving hydrogen sulphide stripping tower, separately leading up to the depriving hydrogen sulphide stripping tower of pipeline and contiguous diesel hydrotreating unit or gasoline hydrogenation device depriving hydrogen sulphide stripping tower is connected.
In the present invention, described cold high pressure separator also has top exit end, be connected by return line between top exit end and described stock oil pipeline, described return line is disposed with desulphurization of recycle hydrogen tower and circulating hydrogen compressor along from cold high pressure separator top exit end on the direction of stock oil pipeline, the hydrogen sulfide that desulphurization of recycle hydrogen tower is brought out by poor amine liquid and the cold high pressure separator top exit of splendid attire in tower carries out desulphurization reaction, the pipeline section of described return line after circulating hydrogen compressor be the pipeline that is connected with the entrance end of described hydrogenator of collateral branch one tunnel also.
In the present invention, described dry gas discharge pipe is also provided with hydrogen rich gas thionizer.
In the present invention, between described high pressure hot separator top exit end and the entrance end of cold high pressure separator, be also provided with hot high score gas air cooler.
In the present invention, between the top exit end of described thermal low-pressure separators and the entrance end of cold low separator, be also provided with heat low point of gas air cooler.
In the present invention, the pipeline section of described stock oil pipeline before the top inlet end of hydrogenator is also provided with reaction heating furnace, for the mixing raw material oil in heating raw oil line.
The present invention is by transforming the circuit flow process of existing hydrogenation unit, increase the bypass flow process of product separation column and fractionation furnace system, by the light oil of cold for device low point, be mainly petroleum naphtha and diesel oil component, change contiguous diesel hydrotreating unit process, to stop the fractionating system of wax oil hydrogenation, utilize the fractionating system of diesel hydrotreating unit to be separated with diesel oil petroleum naphtha.Oil at the bottom of depriving hydrogen sulphide stripping tower tower is directly delivered to stock oil heat exchange after, cold wax oil goes to tank field through air cooling, and hot wax oil removes catalytic unit.Produce because wax oil hydrogenation stripping return tank of top of the tower still has part petroleum naphtha, contiguous diesel hydrotreating unit gasoline desulfur hydrogen stripping tower or the gasoline desulfur hydrogen stripping tower of gasoline hydrogenation device can be caused by adapter line.By above transformation, can stop fractionation process furnace, and the pumps such as Fractionator Bottom pump, diesel oil column bottoms pump, fractionation tower top reflux pump and separation column head space cooler of stopping using, reduce plant energy consumption.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.
Fig. 1 is the one-piece construction figure of Wax Oil Hydrogenation Unit in prior art;
Fig. 2 is the one-piece construction figure of Wax Oil Hydrogenation Unit of the present invention.
Description of reference numerals
1, reaction heating furnace; 2, hydrogenator; 3, high pressure hot separator;
4, thermal low-pressure separators; 5, cold high pressure separator; 6, cold low separator;
7, depriving hydrogen sulphide stripping tower; 8, hydrogen rich gas thionizer; 9, desulphurization of recycle hydrogen tower;
10, circulating hydrogen compressor; 11, hot high score gas air cooler; 12, heat low point of gas air cooler;
13, depriving hydrogen sulphide stripping return tank of top of the tower; 14, fractionation process furnace; 15, separation column;
16, fractionation return tank of top of the tower; 17, diesel oil stripping tower
Embodiment
Energy-saving Wax Oil Hydrogenation Unit in petrochemical complex as shown in Figure 2, comprise reaction heating furnace 1, hydrogenator 2, oil product separating unit, depriving hydrogen sulphide stripping tower 7 and depriving hydrogen sulphide stripping return tank of top of the tower 13, after reaction heating furnace 1, entered the top inlet end of hydrogenator 2 by stock oil pipeline containing the mixing raw material oil of decompressed wax oil and catalytic diesel oil, reaction heating furnace 1 is arranged on the pipeline section of stock oil pipeline before the top inlet end of hydrogenator 2, for the mixing raw material oil in heating raw oil line, mixing raw material oil carries out hydrogenation reaction in hydrogenator 2, generation comprises petroleum naphtha, refine the mixing oil product of wax oil and diesel oil and comprise hydrogen sulfide and methane, the mixed gas of ethane.
Oil product separating unit is by high pressure hot separator 3, thermal low-pressure separators 4, cold high pressure separator 5 and cold low separator 6 form, the exit end of hydrogenator 2 is connected with the entrance end of high pressure hot separator 3, the exit end of high pressure hot separator 3 is divided into two-way, top exit end is connected with the entrance end of cold high pressure separator 5, hot high score gas air cooler 11 is also provided with between high pressure hot separator 3 top exit end and the entrance end of cold high pressure separator 5, the outlet at bottom end of high pressure hot separator 3 is connected with the entrance end of thermal low-pressure separators 4, the product that hydrogenator 2 hydrogenation reaction obtains is separated in high pressure hot separator 3, the refining wax oil that proportion is heavier and a small amount of diesel oil enter in thermal low-pressure separators 4, the petroleum naphtha that proportion is lighter, comprise hydrogen sulfide and methane, mixed gas and a large amount of diesel oil of ethane enter cold high pressure separator 5, the exit end of cold high pressure separator 5 is divided into two-way, be respectively outlet at bottom end and top exit end, be connected by return line between top exit end with stock oil pipeline, return line is disposed with desulphurization of recycle hydrogen tower 9 and circulating hydrogen compressor 10 along from cold high pressure separator 5 top exit end on the direction of stock oil pipeline, the hydrogen sulfide that desulphurization of recycle hydrogen tower 9 is brought out by poor amine liquid and cold high pressure separator 5 top exit of splendid attire in tower carries out desulphurization reaction, the pipeline section of return line after circulating hydrogen compressor 10 be the pipeline that is connected with the entrance end of hydrogenator 2 of collateral branch one tunnel also, the hydrogen that desulphurization reaction is produced adds in hydrogenator 2 again, the outlet at bottom end of cold high pressure separator 5 is connected with the entrance end of cold low separator 6, the exit end of thermal low-pressure separators 4 is divided into two-way, top exit end is connected with the entrance end of cold low separator 6, heat low point of gas air cooler 12 is also provided with between the top exit end of thermal low-pressure separators 4 and the entrance end of cold low separator 6, the outlet at bottom end of thermal low-pressure separators 4 is connected with depriving hydrogen sulphide stripping tower 7 by pipeline, the oil product entering depriving hydrogen sulphide stripping tower 7 from thermal low-pressure separators 4 outlet at bottom end is essentially refining wax oil, a small amount of diesel oil enters cold low separator 6 by top exit end.
The petroleum naphtha that cold low separator 6 will obtain, diesel oil and comprise hydrogen sulfide and methane, the mixed gas of ethane is separated, the exit end of cold low separator 6 is divided into two-way, top exit end is connected with dry gas discharge pipe, by dry gas discharge pipe by the methane in mixed gas, ethane gas is discharged, cold low separator 6 outlet at bottom end is connected with diesel hydrotreating unit by pipeline, the mixing oil product of the diesel oil higher for output purity and petroleum naphtha, depriving hydrogen sulphide stripping tower 7 is connected with depriving hydrogen sulphide stripping return tank of top of the tower 13, the top exit end of depriving hydrogen sulphide stripping tower 7 is connected by pipeline with depriving hydrogen sulphide stripping return tank of top of the tower 13, the outlet at bottom end of depriving hydrogen sulphide stripping tower 7 is connected with wax oil pipeline, for exporting refining wax oil, containing a small amount of petroleum naphtha and mixed gas in depriving hydrogen sulphide stripping return tank of top of the tower 13, by depriving hydrogen sulphide stripping return tank of top of the tower 13 by petroleum naphtha, hydrogen sulfide in mixed gas and methane, ethane separation.
The outlet of depriving hydrogen sulphide stripping return tank of top of the tower 13 is divided into three tunnels, one tunnel is connected with dry gas discharge pipe, for exporting the methane after separation and ethane, one tunnel is connected with the top of depriving hydrogen sulphide stripping tower 7, a partitioning cycle loop is formed with depriving hydrogen sulphide stripping tower 7, circulation desulfurization hydrogen is carried out for being back to again in depriving hydrogen sulphide stripping tower 7 by the hydrogen sulfide after separation, separately leading up to the depriving hydrogen sulphide stripping tower of pipeline and contiguous diesel hydrotreating unit or gasoline hydrogenation device depriving hydrogen sulphide stripping tower is connected, for exporting the petroleum naphtha after separation.
Dry gas discharge pipe in the present embodiment is also provided with hydrogen rich gas thionizer 8, for absorbing from the hydrogen sulfide of cold low separator 6 and depriving hydrogen sulphide stripping return tank of top of the tower 13, methane and ethane mixed gas, hydrogen rich gas thionizer 8 carries out desulphurization reaction by the poor amine liquid of splendid attire in tower and hydrogen sulfide, obtains methane and the ethane mixed gas of purification.
Compared with existing Wax Oil Hydrogenation Unit, Wax Oil Hydrogenation Unit cold low separator of the present invention petroleum naphtha out and diesel oil are not enter in depriving hydrogen sulphide stripping tower 7, but are directly changed to the cold low subentry of contiguous diesel hydrotreating unit or cold low point of oil export; Petroleum naphtha simultaneously in depriving hydrogen sulphide stripping return tank of top of the tower 13 changes the sour gasoline depriving hydrogen sulphide stripping tower process of contiguous diesel hydrotreating unit or changes contiguous gasoline hydrogenation device depriving hydrogen sulphide stripping tower process.
In Wax Oil Hydrogenation Unit of the present invention, Wax Oil Hydrogenation Unit is refined wax oil and is changed into after stripping tower and directly enter tank field or direct-furnish catalytic cracking unit, bypasses point furnace and separation column.Transformation increases wax oil hydrogenation cold low separator oil and goes diesel hydrotreating unit cold low separator flow process, utilizes the fractionating system of diesel hydrotreating unit to be separated with diesel oil petroleum naphtha; Transformation increases wax oil hydrogenation stripping return tank of top of the tower oil part and goes contiguous gasoline hydrogenation device or diesel hydrotreating unit gasoline desulfur hydrogen stripping tower flow process.The present invention can realize Wax Oil Hydrogenation Unit simplification of flowsheet, and the equipment of separation column part of stopping using, significantly reduces plant energy consumption.
Wax Oil Hydrogenation Unit of the present invention is after transformation, device is stopped using and is divided a furnace one, inactive fractionating column system, stop Fractionator Bottom pump, diesel oil pump, fractionation tower top reflux pump, stop diesel oil air cooling two, amount to oil fuel and can reduce 6937.2 tons every year, amount to fuel cost and can reduce 2292.05 ten thousand yuan every year, after transformation, product diesel oil delivers to catalytic unit with product purification wax oil, takies the processing power of catalytic unit; The diesel oil amount delivering to catalytic unit after transformation is every year 79185.6 tons, and catalytic unit fuel cost increases by 1292.71 ten thousand yuan/year.Effect can be created every year: 2292.05-1292.71=999.34 ten thousand yuan.
The above embodiment of the present invention is not limiting the scope of the present invention; embodiments of the present invention are not limited thereto; all this kind is according to foregoing of the present invention; according to ordinary technical knowledge and the customary means of this area; do not departing under the present invention's above-mentioned basic fundamental thought prerequisite; to the amendment of other various ways that said structure of the present invention is made, replacement or change, all should drop within protection scope of the present invention.
Claims (6)
1. energy-saving Wax Oil Hydrogenation Unit in petrochemical complex, comprise hydrogenator (2), oil product separating unit, depriving hydrogen sulphide stripping tower (7) and depriving hydrogen sulphide stripping return tank of top of the tower (13), described oil product separating unit is by high pressure hot separator (3), thermal low-pressure separators (4), cold high pressure separator (5) and cold low separator (6) composition, the exit end of described hydrogenator (2) is connected with the entrance end of high pressure hot separator (3), the exit end of high pressure hot separator (3) is divided into two-way, top exit end is connected with the entrance end of cold high pressure separator (5), outlet at bottom end is connected with the entrance end of thermal low-pressure separators (4), described cold high pressure separator (5) has outlet at bottom end, outlet at bottom end is connected with the entrance end of cold low separator (6), the exit end of described thermal low-pressure separators (4) is divided into two-way, top exit end is connected with the entrance end of cold low separator (6), outlet at bottom end is connected with depriving hydrogen sulphide stripping tower (7) by pipeline, the exit end of described cold low separator (6) is divided into two-way, top exit end is connected with dry gas discharge pipe, it is characterized in that: described cold low separator (6) outlet at bottom end is connected with diesel hydrotreating unit by pipeline, described depriving hydrogen sulphide stripping tower (7) is connected with depriving hydrogen sulphide stripping return tank of top of the tower (13), the top exit end of depriving hydrogen sulphide stripping tower (7) is connected by pipeline with depriving hydrogen sulphide stripping return tank of top of the tower (13), the outlet at bottom end of depriving hydrogen sulphide stripping tower (7) is connected with wax oil pipeline, the outlet of described depriving hydrogen sulphide stripping return tank of top of the tower (13) is divided into three tunnels, one tunnel is connected with described dry gas discharge pipe, one tunnel is connected with the top of depriving hydrogen sulphide stripping tower (7), a partitioning cycle loop is formed with depriving hydrogen sulphide stripping tower (7), separately leading up to the depriving hydrogen sulphide stripping tower of pipeline and contiguous diesel hydrotreating unit or gasoline hydrogenation device depriving hydrogen sulphide stripping tower is connected.
2. energy-saving Wax Oil Hydrogenation Unit in petrochemical complex according to claim 1, it is characterized in that: described cold high pressure separator (5) also has top exit end, be connected by return line between top exit end and described stock oil pipeline, described return line is disposed with desulphurization of recycle hydrogen tower (9) and circulating hydrogen compressor (10) along from cold high pressure separator (5) top exit end on the direction of stock oil pipeline, the hydrogen sulfide that desulphurization of recycle hydrogen tower (9) is brought out by poor amine liquid and cold high pressure separator (5) top exit of splendid attire in tower carries out desulphurization reaction, the pipeline section of described return line after circulating hydrogen compressor (10) be the pipeline that is connected with the entrance end of described hydrogenator (2) of collateral branch one tunnel also.
3. energy-saving Wax Oil Hydrogenation Unit in petrochemical complex according to claim 1, is characterized in that: described dry gas discharge pipe is also provided with hydrogen rich gas thionizer (8).
4. energy-saving Wax Oil Hydrogenation Unit in petrochemical complex according to claim 1, is characterized in that: be also provided with hot high score gas air cooler (11) between the entrance end of described high pressure hot separator (3) top exit end and cold high pressure separator (5).
5. energy-saving Wax Oil Hydrogenation Unit in petrochemical complex according to claim 1, is characterized in that: be also provided with heat low point of gas air cooler (12) between the top exit end of described thermal low-pressure separators (4) and the entrance end of cold low separator (6).
6. energy-saving Wax Oil Hydrogenation Unit in the petrochemical complex according to any one of claim 1 to 5, it is characterized in that: the pipeline section of described stock oil pipeline before the top inlet end of hydrogenator (2) is also provided with reaction heating furnace (1), for the mixing raw material oil in heating raw oil line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410520678.2A CN104312625A (en) | 2014-09-30 | 2014-09-30 | Energy-saving type wax oil hydrogenation equipment in petrochemical industry |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410520678.2A CN104312625A (en) | 2014-09-30 | 2014-09-30 | Energy-saving type wax oil hydrogenation equipment in petrochemical industry |
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| CN104312625A true CN104312625A (en) | 2015-01-28 |
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| CN201410520678.2A Pending CN104312625A (en) | 2014-09-30 | 2014-09-30 | Energy-saving type wax oil hydrogenation equipment in petrochemical industry |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109181769A (en) * | 2018-11-13 | 2019-01-11 | 唐山冀油瑞丰化工有限公司 | Energy-saving Wax Oil Hydrogenation Unit in petrochemical industry |
| CN109266379A (en) * | 2018-11-30 | 2019-01-25 | 山东齐胜工贸股份有限公司 | A kind of desulfurizing oil technique |
| CN111996035A (en) * | 2020-09-14 | 2020-11-27 | 中国石化北海炼化有限责任公司 | Wax oil hydrogenation upgrading system |
| CN113736517A (en) * | 2021-10-27 | 2021-12-03 | 山东东方华龙工贸集团有限公司 | Cracking stripping tower |
| CN113831935A (en) * | 2020-06-23 | 2021-12-24 | 中国石油化工股份有限公司 | Hydrocracking device |
| CN115228245A (en) * | 2022-07-19 | 2022-10-25 | 金澳科技（湖北）化工有限公司 | Method and device for recycling liquid-phase hydrogenation cold low-split gas of diesel wax oil |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102899081A (en) * | 2011-07-28 | 2013-01-30 | 中国石油化工股份有限公司 | Wax oil hydrotreating method |
| CN103773495A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrotreatment-catalytic cracking combination process method |
-
2014
- 2014-09-30 CN CN201410520678.2A patent/CN104312625A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102899081A (en) * | 2011-07-28 | 2013-01-30 | 中国石油化工股份有限公司 | Wax oil hydrotreating method |
| CN103773495A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrotreatment-catalytic cracking combination process method |
Non-Patent Citations (1)
| Title |
|---|
| 杨云平等: ""蜡油加氢装置流程设计优化"", 《中外能源》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109181769A (en) * | 2018-11-13 | 2019-01-11 | 唐山冀油瑞丰化工有限公司 | Energy-saving Wax Oil Hydrogenation Unit in petrochemical industry |
| CN109181769B (en) * | 2018-11-13 | 2021-02-19 | 唐山冀油瑞丰化工有限公司 | Energy-saving wax oil hydrogenation device in petrochemical industry |
| CN109266379A (en) * | 2018-11-30 | 2019-01-25 | 山东齐胜工贸股份有限公司 | A kind of desulfurizing oil technique |
| CN113831935A (en) * | 2020-06-23 | 2021-12-24 | 中国石油化工股份有限公司 | Hydrocracking device |
| CN111996035A (en) * | 2020-09-14 | 2020-11-27 | 中国石化北海炼化有限责任公司 | Wax oil hydrogenation upgrading system |
| CN113736517A (en) * | 2021-10-27 | 2021-12-03 | 山东东方华龙工贸集团有限公司 | Cracking stripping tower |
| CN115228245A (en) * | 2022-07-19 | 2022-10-25 | 金澳科技（湖北）化工有限公司 | Method and device for recycling liquid-phase hydrogenation cold low-split gas of diesel wax oil |
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